EP0010814A1 - Process for the preparation of pulverulent thermoplastic copolymers of ethylene and 1-butene - Google Patents
Process for the preparation of pulverulent thermoplastic copolymers of ethylene and 1-butene Download PDFInfo
- Publication number
- EP0010814A1 EP0010814A1 EP79200632A EP79200632A EP0010814A1 EP 0010814 A1 EP0010814 A1 EP 0010814A1 EP 79200632 A EP79200632 A EP 79200632A EP 79200632 A EP79200632 A EP 79200632A EP 0010814 A1 EP0010814 A1 EP 0010814A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- butene
- compounds
- ethylene
- vanadyl
- aluminum
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 21
- 239000005977 Ethylene Substances 0.000 title claims abstract description 21
- 238000000034 method Methods 0.000 title claims abstract description 17
- 229920001169 thermoplastic Polymers 0.000 title claims abstract description 5
- 239000004416 thermosoftening plastic Substances 0.000 title claims abstract description 5
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 title claims description 12
- 238000002360 preparation method Methods 0.000 title abstract description 3
- 150000001875 compounds Chemical class 0.000 claims abstract description 13
- 125000005287 vanadyl group Chemical group 0.000 claims abstract description 13
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 12
- 239000003054 catalyst Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 7
- 239000001257 hydrogen Substances 0.000 claims abstract description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 3
- 125000003545 alkoxy group Chemical group 0.000 claims abstract description 3
- 239000000460 chlorine Substances 0.000 claims abstract description 3
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 3
- 238000006116 polymerization reaction Methods 0.000 claims description 12
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims description 8
- 239000000843 powder Substances 0.000 claims description 7
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 6
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 5
- 229910052782 aluminium Inorganic materials 0.000 claims description 5
- UAIZDWNSWGTKFZ-UHFFFAOYSA-L ethylaluminum(2+);dichloride Chemical compound CC[Al](Cl)Cl UAIZDWNSWGTKFZ-UHFFFAOYSA-L 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 5
- -1 unsaturated C 4 hydrocarbons Chemical class 0.000 claims description 5
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 claims description 4
- 125000005234 alkyl aluminium group Chemical group 0.000 claims description 4
- YNLAOSYQHBDIKW-UHFFFAOYSA-M diethylaluminium chloride Chemical compound CC[Al](Cl)CC YNLAOSYQHBDIKW-UHFFFAOYSA-M 0.000 claims description 4
- 150000003682 vanadium compounds Chemical class 0.000 claims description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- CMAOLVNGLTWICC-UHFFFAOYSA-N 2-fluoro-5-methylbenzonitrile Chemical compound CC1=CC=C(F)C(C#N)=C1 CMAOLVNGLTWICC-UHFFFAOYSA-N 0.000 claims description 2
- NMVXHZSPDTXJSJ-UHFFFAOYSA-L 2-methylpropylaluminum(2+);dichloride Chemical compound CC(C)C[Al](Cl)Cl NMVXHZSPDTXJSJ-UHFFFAOYSA-L 0.000 claims description 2
- 239000004215 Carbon black (E152) Substances 0.000 claims description 2
- 230000003213 activating effect Effects 0.000 claims description 2
- 230000004913 activation Effects 0.000 claims description 2
- HQMRIBYCTLBDAK-UHFFFAOYSA-M bis(2-methylpropyl)alumanylium;chloride Chemical compound CC(C)C[Al](Cl)CC(C)C HQMRIBYCTLBDAK-UHFFFAOYSA-M 0.000 claims description 2
- 125000004432 carbon atom Chemical group C* 0.000 claims description 2
- 238000010924 continuous production Methods 0.000 claims description 2
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 4
- 230000000379 polymerizing effect Effects 0.000 abstract description 3
- 229910052736 halogen Inorganic materials 0.000 abstract 2
- 150000002367 halogens Chemical class 0.000 abstract 2
- 239000012190 activator Substances 0.000 abstract 1
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 30
- 229920000642 polymer Polymers 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 229920001577 copolymer Polymers 0.000 description 6
- 239000003085 diluting agent Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 238000007334 copolymerization reaction Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000000725 suspension Substances 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- LFXVBWRMVZPLFK-UHFFFAOYSA-N trioctylalumane Chemical compound CCCCCCCC[Al](CCCCCCCC)CCCCCCCC LFXVBWRMVZPLFK-UHFFFAOYSA-N 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- 229920000573 polyethylene Polymers 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- MCULRUJILOGHCJ-UHFFFAOYSA-N triisobutylaluminium Chemical compound CC(C)C[Al](CC(C)C)CC(C)C MCULRUJILOGHCJ-UHFFFAOYSA-N 0.000 description 2
- 229910052720 vanadium Inorganic materials 0.000 description 2
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 2
- 235000007487 Calathea allouia Nutrition 0.000 description 1
- 244000278792 Calathea allouia Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- IAQRGUVFOMOMEM-ARJAWSKDSA-N cis-but-2-ene Chemical compound C\C=C/C IAQRGUVFOMOMEM-ARJAWSKDSA-N 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000003701 inert diluent Substances 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 229920001684 low density polyethylene Polymers 0.000 description 1
- 239000004702 low-density polyethylene Substances 0.000 description 1
- 238000001000 micrograph Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000002685 polymerization catalyst Substances 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- IAQRGUVFOMOMEM-ONEGZZNKSA-N trans-but-2-ene Chemical compound C\C=C\C IAQRGUVFOMOMEM-ONEGZZNKSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F210/14—Monomers containing five or more carbon atoms
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F210/00—Copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F210/16—Copolymers of ethene with alpha-alkenes, e.g. EP rubbers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S526/00—Synthetic resins or natural rubbers -- part of the class 520 series
- Y10S526/903—Monomer polymerized in presence of transition metal containing catalyst and hydrocarbon additive affecting polymer properties of catalyst activity
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10T—TECHNICAL SUBJECTS COVERED BY FORMER US CLASSIFICATION
- Y10T428/00—Stock material or miscellaneous articles
- Y10T428/29—Coated or structually defined flake, particle, cell, strand, strand portion, rod, filament, macroscopic fiber or mass thereof
- Y10T428/2982—Particulate matter [e.g., sphere, flake, etc.]
Definitions
- the invention relates to a process for the production of thermoplastic copolymers of low-density ethylene as processable powders of relatively high bulk densities by copolymerization of ethylene and butene (I) with the aid of Ziegler catalysts containing vanadium.
- low density ethylene polymers is usually carried out by polymerizing ethylene with free radical initiation under high pressures of 1,000 bar to 3,000 bar.
- These processes have the disadvantage that the generation of high pressures is technically complex and costly.
- Another disadvantage of these methods is that they cannot be used to produce polymers with such high molecular weights that they have satisfactory properties such as, for example, good stress crack resistance to surface-active media or high breaking strength under alternating bending stress and others. Because of their relatively low molecular weights, the ethylene polymers produced by the high-pressure processes are therefore not suitable for all areas of use.
- copolymers of low densities from ethylene and butene- (1) can also be produced as free-flowing powders with relatively high bulk densities if liquid butene- (1) is used as an inert diluent, which may also include other inert saturated and / or may contain unsaturated C 4 hydrocarbons.
- the invention therefore relates to a process for the preparation of powdered thermoplastic copolymers of ethylene and butene- (1) with densities of about 0.900 g / cm 3 to about 0.930 g / cm 3 , good flowability of the powder, average leren grain diameters up to 1000 microns and practically no fine grain content by polymerization of ethylene and butene- (1), optionally in the presence of hydrogen, in inert liquid hydrocarbons at temperatures between 50 ° C and about 95 ° C and pressures from 10 bar to 100 bar, preferably 20 bar to 60 bar, by batch or continuous process using Ziegler catalysts, produced in inert liquid hydrocarbons by reacting vanadyl (V) compounds containing chlorine and alkoxy with organoaluminum compounds, separating off the insoluble reaction product and activating with organoaluminum compounds, where as the vanadyl (v) compound a reaction product of vanadyl (V) chloride and a vanadyl (V) alcoholate in
- 1 to 20,000 watts / m 3 preferably 1 to 5,000 watts / m 3
- the activation with aluminum alkyl compounds of the formula AIR 3 in which R is hydrocarbon radicals with 2 to 8 carbon atoms, or with alkyl aluminum sesquichloride and / or alkyl aluminum dichloride , in particular ethyl aluminum sesquichloride and / or ethyl aluminum dichloride, characterized in that polymerization is carried out in liquid butene (1), if appropriate in the presence of further inert, saturated and / or unsaturated C 4 hydrocarbons.
- polymerization is preferably carried out using pure butene- (1).
- the commercial purity is 99 percent.
- a C 4 - can also be used according to the invention.
- Section which may contain, for example, butene (1), trans and cis-butene (2), isobutene, n-butane and isobutane. It is important that the admixtures are indifferent to the polymerization catalyst.
- the mixture should preferably not contain any butadiene (1,3), which has proven to be a catalyst poison.
- care must be taken that "the molar ratio of butene (1) to ethylene required for the desired density of the copolymer in the polymerization is observed.
- the process according to the present invention surprisingly offers the possibility of using the catalyst system known from Belgian patent 862,697 to also produce copolymers of ethylene and butene- (1) with significantly lower densities than those described in the Belgian patent, the polymers being in the form of a powder Diluents are obtained in suspension and, after their separation from the suspension, are suitable for further processing into finished plastic parts after addition of the customary finishing aids, so that the otherwise necessary processing of the polymers into granules can be omitted. Since very high conversions can be achieved with the catalysts used according to the invention, measures for removing the catalyst from the polymer can be dispensed with.
- the low-density copolymers produced according to the invention have excellent performance properties.
- pipes made from the copolymers produced according to the invention have high burst pressures and excellent flexural strength.
- Injection molded parts show an excellent surface gloss and have no tendency to shrink and warp.
- Films made from the copolymers produced according to the invention are notable for special shock resistance and elongation at break.
- Example 2 The procedure was analogous to Example 1. Instead of triisobutyl aluminum, however, tri-n-octyl aluminum was used as the cocatalyst. 2.2 ml of a solution in hexane with a concentration of 167 g of tri-n-octylaluminum per liter were used. The amount of the solid catalyst component was 20 mg, the hydrogen partial pressure 1.0 bar, the total pressure 33 bar. The polymerization was carried out at 60 ° C. for 4 hours. The polymer consisted of a free-flowing powder. Further information can be found in Table 4.
Abstract
Ein Verfahren zur Herstellung von pulverförmigen, thermoplastischen Copolymeren aus Äthylen und Buten-(1) mit guter Rieselfähigkeit durch Polymerisation von Äthylen und Buten-(1) in inerten Kohlenwasserstoffen bei üblichen Temperaturen und Drücken und gegebenenfalls in Gegenwart von Wasserstoff mittels Ziegler-Katalysatoren, bestehend aus dem unlöslichen Reaktionsprodukt von chlor- und alkoxyhaltigen Vanadyl(V)-Verbindungen mit halogenhaltigen aluminiumorganischen Verbindungen und weiteren, gegebenenfalls halogenhaltigen aluminiumorganischen Verbindungen als Aktivator, wobei man in flüssigem Buten-(1), gegebenenfalls in Gegenwart weiterer C4-Kohlenwasserstoffe polymerisiert.A process for the preparation of powdery, thermoplastic copolymers of ethylene and butene- (1) with good flow properties by polymerizing ethylene and butene- (1) in inert hydrocarbons at customary temperatures and pressures and, if appropriate, in the presence of hydrogen using Ziegler catalysts from the insoluble reaction product of chlorine and alkoxy-containing vanadyl (V) compounds with halogen-containing organoaluminum compounds and further, optionally halogen-containing organo-aluminum compounds as activators, polymerizing in liquid butene- (1), optionally in the presence of further C4-hydrocarbons.
Description
Die Erfindung betrifft ein Verfahren zur Herstellung von thermoplastischen Copolymeren des Äthylens niedriger Dichte als verarbeitbare Pulver relativ hoher Schüttdichten durch Copolymerisation von Äthylen und Buten-(l) mit Hilfe von Vanadin enthaltenden Ziegler-Katalysatoren.The invention relates to a process for the production of thermoplastic copolymers of low-density ethylene as processable powders of relatively high bulk densities by copolymerization of ethylene and butene (I) with the aid of Ziegler catalysts containing vanadium.
Die Herstellung von Äthylenpolymerisaten niedriger Dichte wird üblicherweise durch Polymerisation von Äthylen mit radikalischer Initiierung unter hohen Drücken von 1 000 bar bis 3 000 bar hergestellt. Diese Verfahren sind einmal mit dem Nachteil verbunden, daß die Erzeugung hoher Drücke technisch aufwendig und kostspielig ist. Ein anderer Nachteil dieser Verfahren besteht darin, daß sich nach ihnen keine Polymerisate mit so hohen Molgewichten erzeugen lassen, daß sie befriedigende Eigenschaften aufweisen wie beispielsweise gute Spannungsrißbeständigkeit gegenüber oberflächenaktiven Medien oder hohe Bruchfestigkeit bei Wechselbiegebeanspruchung und andere mehr. Die nach den Hochdruckverfahren hergestellten Äthylenpolymerisate sind also wegen ihrer relativ niedrigen Molgewichte nicht für alle Einsatzgebiete verwendbar.The production of low density ethylene polymers is usually carried out by polymerizing ethylene with free radical initiation under high pressures of 1,000 bar to 3,000 bar. These processes have the disadvantage that the generation of high pressures is technically complex and costly. Another disadvantage of these methods is that they cannot be used to produce polymers with such high molecular weights that they have satisfactory properties such as, for example, good stress crack resistance to surface-active media or high breaking strength under alternating bending stress and others. Because of their relatively low molecular weights, the ethylene polymers produced by the high-pressure processes are therefore not suitable for all areas of use.
Weiterhin ist ein Verfahren bekannt geworden zur Herstellung von niedrigdichtem Polyäthylen mit Dichten von 0,915 g/cm3 bis 0,930 g/cm3 durch Copolymerisation von Äthylen mit (1)-Olefinen in Hexan bei Temperaturen >130 °C. Bei diesem Verfahren ist es von Nachteil, daß das Polymerisat in Hexan gelöst anfällt und aus dem Lösungsmittel abgetrennt werden muß.Furthermore, a method has become known for the production of low-density polyethylene with densities of 0.915 g / cm 3 to 0.930 g / cm 3 by copolymerization of ethylene with (1) -olefins in hexane at temperatures> 130 ° C. In this process, it is disadvantageous that the polymer is obtained in solution in hexane and must be separated from the solvent.
In letzter Zeit ist durch das belgische Patent 862.697 ein Verfahren bekannt geworden, bei dem aus Äthylen und gegebenenfalls (l)-Olefinen als Comonomere durch Polymerisation mit Vanadin enthaltenden Katalysatoren in inerten flüssigen Kohlenwasserstoffen bei Temperaturen von 50 °C bis etwa 95 °C und Drücken von 10 bar bis 100 bar pulverförmige Polymerisate mit hervorragenden Eigenschaften für die Weiterverarbeitung zu Fertigteilen hergestellt werden können. Als Verdünnungsmittel bei der Polymerisation wurden flüssige inerte Kohlenwasserstoffe, vorzugsweise ein Hexanschnitt mit dem Siedebereich von 63 °C bis 80 °C, genannt. Unter Verwendung derartiger Verdünnungsmittel lassen sich jedoch keine pulverförmigen Polymerisate aus Äthylen und Buten-(1) mit Dichten von etwa 0,900 g/cm3 bis etwa 0,930 g/em3 herstellen. Die Polymerisate fallen vielmehr als Brocken und Klumpen an und lassen sich in einer technischen Apparatur nicht hantieren.A process has recently become known from Belgian patent 862,697 in which ethylene and optionally (l) -olefins as comonomers are polymerized by polymerization with vanadium-containing catalysts in inert liquid hydrocarbons at temperatures from 50 ° C. to about 95 ° C. and pressures from 10 bar to 100 bar powdered polymers with excellent properties for further processing into finished parts. Liquid inert hydrocarbons, preferably a hexane cut with the boiling range from 63 ° C. to 80 ° C., were mentioned as diluents in the polymerization. However, using such diluents, it is not possible to prepare pulverulent polymers of ethylene and butene- (1) with densities of about 0.900 g / cm 3 to about 0.930 g / em 3 . Rather, the polymers accumulate as lumps and lumps and cannot be handled in technical equipment.
Demgegenüber wurde nunmehr gefunden, daß man Copolymere niedriger Dichten aus Äthylen und Buten-(1) auch als rieselfähige Pulver mit relativ hohen Schüttdichten herstellen kann, wenn man als inertes Verdünnungsmittel flüssiges Buten-(1) verwendet, das gegebenenfalls auch andere inerte gesättigte und/ oder ungesättigte C4-Kohlenwasserstoffe enthalten kann.In contrast, it has now been found that copolymers of low densities from ethylene and butene- (1) can also be produced as free-flowing powders with relatively high bulk densities if liquid butene- (1) is used as an inert diluent, which may also include other inert saturated and / or may contain unsaturated C 4 hydrocarbons.
Gegenstand der Erfindung ist daher ein Verfahren zur Herstellung von pulverförmigem thermoplastischen Copolymeren aus Äthylen und Buten-(1) mit Dichten von etwa 0,900 g/cm3 bis etwa 0,930 g/cm3, guter Rieselfähigkeit des Pulvers, mittleren Korndurchmessern bis zu 1 000 um und praktisch ohne Feinstkornanteil durch Polymerisation von Äthylen und Buten-(1), gegebenenfalls in Gegenwart von Wasserstoff, in inerten flüssigen Kohlenwasserstoffen bei Temperaturen zwischen 50 °C und etwa 95 °C und Drücken von 10 bar bis 100 bar, vorzugsweise 20 bar bis 60 bar, nach diskontinuierlichem oder kontinuierlichem Verfahren mittels Ziegler-Katalysatoren, hergestellt in inerten flüssigen Kohlenwasserstoffen durch Umsetzung chlor- und alkoxyhaltiger Vanadyl(V)-verbindungen mit aluminiumorganischen Verbindungen, Abtrennung des unlöslichen Reaktionsproduktes und Aktivierung mit aluminiumorganischen Verbindungen, wobei als Vanadyl(v)-verbindung ein Umsetzungsprodukt von Vanadyl(V)-chlorid und einem Vanadyl(V)-alkoholat in Molverhältnissen von 1 zu 2 bis 2 zu 1 oder direkt das Umsetzungsprodukt von Vanadyl(V)-chlorid mit einem Alkohol, vorzugsweise Äthanol, Propanol-(l), Butanol-(l) in Molverhältnissen von 1 zu 2 bis 1 zu 1 und als aluminiumorganische Verbindung zur Reduktion Äthylaluminiumdichlorid und/oder Diäthylaluminiumchlorid, Isobutylaluminiumdichlorid und/oder Diisobutylaluminiumchlorid in Molverhältnissen von Aluminium- zu Vanadinverbindungen von 1 zu 1 bis 3 zu 1 verwendet und die Umsetzung der Vanadin-Verbindungen mit den aluminiumorganischen Verbindungen unter Rühren mit spezifischen Rührleistungen von 0,1 bis 20 000 Watt/m3, vorzugsweise 1 bis 5 000 Watt/m3, vorgenommen wird und die Aktivierung mit Aluminiumalkylverbindungen der Formel AIR3, worin R Kohlenwasserstoffreste mit 2 bis 8 C-Atomen bedeuten, oder mit Alkylaluminiumsesquichlorid und/ oder Alkylaluminiumdichlorid, insbesondere Äthylaluminiumsesquichlorid und/oder Äthylaluminiumdichlorid erfolgt, dadurch gekennzeichnet, daß man in flüssigem Buten-(1), gegebenenfalls in Gegenwart weiterer inerter, gesättigter und/oder ungesättigter C4-Kohlenwasserstoffe, polymerisiert.The invention therefore relates to a process for the preparation of powdered thermoplastic copolymers of ethylene and butene- (1) with densities of about 0.900 g / cm 3 to about 0.930 g / cm 3 , good flowability of the powder, average leren grain diameters up to 1000 microns and practically no fine grain content by polymerization of ethylene and butene- (1), optionally in the presence of hydrogen, in inert liquid hydrocarbons at temperatures between 50 ° C and about 95 ° C and pressures from 10 bar to 100 bar, preferably 20 bar to 60 bar, by batch or continuous process using Ziegler catalysts, produced in inert liquid hydrocarbons by reacting vanadyl (V) compounds containing chlorine and alkoxy with organoaluminum compounds, separating off the insoluble reaction product and activating with organoaluminum compounds, where as the vanadyl (v) compound a reaction product of vanadyl (V) chloride and a vanadyl (V) alcoholate in molar ratios of 1 to 2 to 2 to 1 or directly the reaction product of vanadyl (V) chloride with an alcohol, preferably ethanol, propanol (1), butanol (1) in molar ratios of 1 to 2 to 1 to 1 and as aluminum nium organic compound for the reduction of ethyl aluminum dichloride and / or diethyl aluminum chloride, isobutyl aluminum dichloride and / or diisobutyl aluminum chloride in molar ratios of aluminum to vanadium compounds from 1 to 1 to 3 to 1 and the reaction of the vanadium compounds with the organoaluminum compounds with stirring with specific stirring performance of 0. 1 to 20,000 watts / m 3 , preferably 1 to 5,000 watts / m 3 , is carried out and the activation with aluminum alkyl compounds of the formula AIR 3 , in which R is hydrocarbon radicals with 2 to 8 carbon atoms, or with alkyl aluminum sesquichloride and / or alkyl aluminum dichloride , in particular ethyl aluminum sesquichloride and / or ethyl aluminum dichloride, characterized in that polymerization is carried out in liquid butene (1), if appropriate in the presence of further inert, saturated and / or unsaturated C 4 hydrocarbons.
Vorzugsweise wird erfindungsgemäß unter Verwendung von reinem Buten-(l) polymerisiert. Die handelsübliche Reinheit beträgt 99 Prozent. Erfindungsgemäß verwendbar ist aber auch ein C4-Schnitt, der beispielsweise außer Buten-(1), trans- und cis-Buten-(2), Isobuten, n-Butan und Isobutan enthalten kann. Wichtig ist es, daß die Beimengungen sich gegenüber dem Polymerisationskatalysator indifferent verhalten. So sollte das Gemisch beispielsweise möglichst kein Butadien-(1,3) enthalten, welches sich als Katalysatorgift erwiesen hat. Selbstverständlich ist darauf zu achten, daß "das bei der Polymerisation für die gewünschte Dichte des Copolymerisates jeweils erforderliche Molverhältnis von Buten-(1) zu Äthylen eingehalten wird.According to the invention, polymerization is preferably carried out using pure butene- (1). The commercial purity is 99 percent. However, a C 4 - can also be used according to the invention. Section which may contain, for example, butene (1), trans and cis-butene (2), isobutene, n-butane and isobutane. It is important that the admixtures are indifferent to the polymerization catalyst. For example, the mixture should preferably not contain any butadiene (1,3), which has proven to be a catalyst poison. Of course, care must be taken that "the molar ratio of butene (1) to ethylene required for the desired density of the copolymer in the polymerization is observed.
Das Verfahren gemäß der vorliegenden Erfindung bietet überraschenderweise die Möglichkeit, mit dem aus der belgischen Patentschrift 862.697 bekannten Katalysatorsystem auch Copolymere aus Äthylen und Buten-(1) mit wesentlich niedrigeren Dichten herzustellen als sie in der belgischen Patentschrift beschrieben sind, wobei die Polymerisate als Pulver im Verdünnungsmittel suspendiert anfallen und nach ihrer Abtrennung aus der Suspension für die Weiterverarbeitung zu Kunststoffertigteilen nach Zusatz der üblichen Konfektionierungshilfsmittel geeignet sind, so daß die sonst notwendige Aufbereitung der Polymerisate zu Granulaten unterbleiben kann. Da sich mit den erfindungsgemäß angewendeten Katalysatoren sehr hohe Umsätze erzielen lassen, kann auf Maßnahmen zur Entfernung des Katalysators aus dem Polymerisat verzichtet werden. Infolge ihrer hohen Molgewichte besitzen die erfindungsgemäß hergestellten Copolymeren niedriger Dichte hervorragende anwendungstechnische Eigenschaften. So weisen aus den erfindungsgemäß hergestellten Copolymeren hergestellte Rohre außer ihrer für manche Anwendungszwecke erforderlichen hohen Flexibilität hohe Berstdrücke und ausgezeichnete Wechselbiegefestigkeiten auf. Spritzgußteile zeigen einen hervorragenden Oberflächenglanz und besitzen keine Neigung zu Schrumpf und Verzug. Aus den erfindungsgemäß hergestellten Copolymeren gefertigte Folien zeichnen sich durch besondere Stoßfestigkeit und Streckdehnung aus.The process according to the present invention surprisingly offers the possibility of using the catalyst system known from Belgian patent 862,697 to also produce copolymers of ethylene and butene- (1) with significantly lower densities than those described in the Belgian patent, the polymers being in the form of a powder Diluents are obtained in suspension and, after their separation from the suspension, are suitable for further processing into finished plastic parts after addition of the customary finishing aids, so that the otherwise necessary processing of the polymers into granules can be omitted. Since very high conversions can be achieved with the catalysts used according to the invention, measures for removing the catalyst from the polymer can be dispensed with. As a result of their high molecular weights, the low-density copolymers produced according to the invention have excellent performance properties. Thus, in addition to the high flexibility required for some applications, pipes made from the copolymers produced according to the invention have high burst pressures and excellent flexural strength. Injection molded parts show an excellent surface gloss and have no tendency to shrink and warp. Films made from the copolymers produced according to the invention are notable for special shock resistance and elongation at break.
Das Verfahren gemäß der vorliegenden Erfindung wird durch die nachstehenden Beispiele illustriert:The method according to the present invention is illustrated by the following examples:
122,3 g (705,7 mMol) Vanadyl(V)-chlorid und 172,3 g (705,7 mMol) Vanadyl(v)-n-propylat wurden zusammen in 1,7 1 eines Hexanschnittes 63/80 °C unter Stickstoff 2 Stunden lang auf 55 °C erhitzt. Nach Abkühlen der Mischung wurde bei 20 °C bis 25 °C eine Lösung von 358,2 g (2 822,8 mMol) Äthylaluminiumdichlorid in 1,43 1 des Hexanschnittes 63/80 °C im Laufe von 2 Stunden unter Rühren mit einem Blattrührer und einer spezifischen Rührleistung von 126 Watt/m3 zugegeben. Die erhaltene Suspension wurde danach noch 2 Stunden bei 55 °C mit gleicher spezifischer Rührleistung gerührt. Nach dem Abkühlen wurde der Feststoff abgetrennt und fünfmal mit je 5 1 des IIexanschnittes gewaschen.122.3 g (705.7 mmol) of vanadyl (V) chloride and 172.3 g (705.7 mmol) of vanadyl (v) -n-propylate were combined in 1.7 1 of a hexane cut at 63/80 ° C Nitrogen heated to 55 ° C for 2 hours. After the mixture had cooled, a solution of 358.2 g (2,822.8 mmol) of ethyl aluminum dichloride in 1.43 l of the hexane cut 63/80 ° C. was stirred at 20 ° C. to 25 ° C. over the course of 2 hours with stirring with a blade stirrer and a specific stirring power of 126 watts / m3. The suspension obtained was then stirred for a further 2 hours at 55 ° C. with the same specific stirring power. After cooling, the solid was separated off and washed five times with 5 liters of the IIexancut.
In einen 2-1-Stahlautoklaven wurden unter Stickstoff 4 ml einer Lösung von Triisobutylaluminium in Hexan mit einer Konzentration von 100 g/1 einpipettiert. Unter Wasserkühlung wurden 600 g Buten-(l) über eine mit Molekularsieb 3 A (Hersteller: Union Carbide) gefüllte Patrone in den Autoklaven gedrückt. Darauf wurde auf die Polymerisationstemperatur aufgeheizt. Zur Entfernung des Stickstoffs wurden über eine Gasuhr 4 Liter Gas abgelassen. Dann wurde Wasserstoff aufgedrückt und danach unter Rühren (1 000 upm) Äthylen. Über eine Schleuse wurde eine Suspension der unter a) beschriebenen Katalysatorkomponente mit einer Konzentration von 10 g Feststoff pro Liter Hexan in den Autoklaven abgelassen. Nach Ablauf der Polymerisationszeit, während der die Polymerisationstemperatur sowie durch Nachfahren von Äthylen der Druck konstant gehalten wurden, wurde auf Raumtemperatur abgekühlt und das überschüssige Buten entspannt. Nähere Angaben zu den einzelnen Beispielen sind den folgenden Tabellen 1 und 2 zu entnehmen.
Abbildungsmaßstab: 16 : 1
Es wurde analog Beispiel 10 verfahren. Davon abweichend wurde als Verdünnungsmittel ein Gemisch aus 79 g Buten-(1), 228 g n-Butan, 214 g trans-Buten-(2), 148 g cis-Buten-(2) verwendet. Die Menge der festen Katalysatorkomponente betrug 44 mg. Die Polymerisation wurde bereits nach einer Stunde abgebrochen. Es wurden 55 g eines gut rieselfähigen pulverförmigen Polymerisates erhalten. Die Eigenschaften sind in der Tabelle 3 aufgeführt.The procedure was analogous to Example 10. Deviating from this, a mixture of 79 g of butene- (1), 228 g of n-butane, 214 g of trans-butene- (2) and 148 g of cis-butene- (2) was used as the diluent. The amount of the solid catalyst component was 44 mg. The polymerization was stopped after one hour. 55 g of a free-flowing powdery polymer were obtained. The properties are listed in Table 3.
Es wurde wie unter lla) verfahren, jedoch mit dem Unterschied, daß als Verdünnungsmittel Hexan 63/80 °C eingesetzt wurde. Die eingesetzte Menge an Buten-(l) betrug 72 g, der Äthylenpartialdruck wie in Beispiel lla) 4,5 bar. Die Ausbeute an Polymerisat betrug 79 g und bestand aus groben Brocken bzw. Klumpen.
Es wurde analog Beispiel 1 verfahren. Anstelle von Triisobutylaluminium wurde jedoch Tri-n-octylaluminium als Cokatalysator angewendet. Eingesetzt wurden 2,2 ml einer Lösung in Hexan mit einer Konzentration von 167 g Tri-n-octylaluminium pro Liter. Die Menge der festen Katalysatorkomponente betrug 20 mg, der Wasserstoffpartialdruck 1,0 bar, der Gesamtdruck 33 bar. Polymerisiert wurde 4 Stunden lang bei 60 °C. Das Polymerisat bestand aus einem rieselfähigen Pulver. Weitere Angaben sind der Tabelle 4 zu entnehmen.The procedure was analogous to Example 1. Instead of triisobutyl aluminum, however, tri-n-octyl aluminum was used as the cocatalyst. 2.2 ml of a solution in hexane with a concentration of 167 g of tri-n-octylaluminum per liter were used. The amount of the solid catalyst component was 20 mg, the hydrogen partial pressure 1.0 bar, the total pressure 33 bar. The polymerization was carried out at 60 ° C. for 4 hours. The polymer consisted of a free-flowing powder. Further information can be found in Table 4.
Es wurde wie bei Beispiel 12 verfahren. Anstelle von Tri-n-octylaluminium wurde aber Diäthylaluminiumchlorid eingesetzt, und zwar 2,2 ml einer Lösung in Hexan mit einer Konzentration von 112 g Diäthylaluminiumchlorid pro Liter. Das Polymerisat bestand aus einem rieselfähigen Pulver. Weitere Angaben sind der Tabelle 4 zu entnehmen.
Claims (1)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19782847986 DE2847986A1 (en) | 1978-11-04 | 1978-11-04 | METHOD FOR PRODUCING POWDER-SHAPED, THERMOPLASTIC COPOLYMERS FROM AETHYLENE AND BUTEN- (1) |
| DE2847986 | 1978-11-04 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0010814A1 true EP0010814A1 (en) | 1980-05-14 |
| EP0010814B1 EP0010814B1 (en) | 1983-06-15 |
Family
ID=6053930
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP79200632A Expired EP0010814B1 (en) | 1978-11-04 | 1979-10-30 | Process for the preparation of pulverulent thermoplastic copolymers of ethylene and 1-butene |
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| Country | Link |
|---|---|
| US (1) | US4294947A (en) |
| EP (1) | EP0010814B1 (en) |
| DE (2) | DE2847986A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2525612A1 (en) * | 1982-04-22 | 1983-10-28 | El Paso Polyolefins | PROCESS FOR PRODUCING LOW-DENSITY LINEAR POLYETHYLENE |
| EP0436520A1 (en) * | 1990-01-03 | 1991-07-10 | Gas Research Institute | Extended-life polyethylene gas distribution pipe |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4508842A (en) * | 1983-03-29 | 1985-04-02 | Union Carbide Corporation | Ethylene polymerization using supported vanadium catalyst |
| IL71356A (en) * | 1983-03-29 | 1987-07-31 | Union Carbide Corp | Process for producing polyethylene,a supported vanadium catalyst precursor therefor and a catalyst composition containing said supported precursor |
| JPS6088016A (en) * | 1983-10-21 | 1985-05-17 | Mitsui Petrochem Ind Ltd | Ethylene copolymer |
| US4754007A (en) * | 1985-03-08 | 1988-06-28 | Enron Chemical Company | Copolymerization of ethylene |
| US5288531A (en) * | 1991-08-09 | 1994-02-22 | The Dow Chemical Company | Pouch for packaging flowable materials |
| US5360648A (en) * | 1993-06-24 | 1994-11-01 | The Dow Chemical Company | Pouch for packaging flowable materials |
| US6015779A (en) | 1996-03-19 | 2000-01-18 | Energy & Environmental International, L.C. | Methods for forming amorphous ultra-high molecular weight polyalphaolefin drag reducing agents |
| US5851945A (en) | 1997-02-07 | 1998-12-22 | Exxon Chemical Patents Inc. | Olefin polymerization catalyst compositions comprising group 5 transition metal compounds stabilized in their highest metal oxidation state |
| US6815011B2 (en) | 2000-11-27 | 2004-11-09 | Energy & Environmental International, L.C. | Alpha olefin monomer partitioning agents for drag reducing agents and methods of forming drag reducing agents using alpha olefin monomer partitioning agents |
| DE60235444D1 (en) | 2001-01-16 | 2010-04-08 | Beta Technologies Ag | METHOD FOR PRODUCING AMORPHOUS POLYOLEFINS WITH ULTRAHIGH MOLECULAR WEIGHT FOR FLOWING ACCELERATION |
| US7012046B2 (en) | 2001-06-08 | 2006-03-14 | Eaton Gerald B | Drag reducing agent slurries having alfol alcohols and processes for forming drag reducing agent slurries having alfol alcohols |
| US7037989B2 (en) * | 2003-05-27 | 2006-05-02 | Exxonmobil Chemical Patents Inc. | Copolymers of ethylene and/or α-olefins and vicinally disubstituted olefins |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE662697A (en) * | 1965-05-20 | 1965-08-17 | ||
| DE2014172A1 (en) * | 1969-03-24 | 1970-10-29 | Phillips Petroleum Company, Bartlesville, OkIa. (V.St.A.) | Ethylene-butene copolymers with low density |
| DE2206429A1 (en) * | 1972-02-11 | 1973-08-30 | Huels Chemische Werke Ag | PROCESS FOR THE PRODUCTION OF LOW PRESSURE CO- AND TERPOLYMERS OF LOW DENSITY ETHYLENE |
| GB1355245A (en) * | 1970-05-29 | 1974-06-05 | Mitsui Petrochemical Ind | Non-elastic ethylene copolymers and their preparation |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2929807A (en) * | 1957-05-13 | 1960-03-22 | Phillips Petroleum Co | Polymerization process for producing copolymers of ethylene and higher 1-olefins |
| GB1415898A (en) * | 1972-02-11 | 1975-12-03 | Huels Chemische Werke Ag | Manufacture of low-density ethylene polymers |
| FR2376876A1 (en) * | 1977-01-07 | 1978-08-04 | Veba Chemie Ag | PROCESS FOR THE MANUFACTURE OF POWDERED POLYOLEFINS |
-
1978
- 1978-11-04 DE DE19782847986 patent/DE2847986A1/en not_active Withdrawn
-
1979
- 1979-10-30 EP EP79200632A patent/EP0010814B1/en not_active Expired
- 1979-10-30 DE DE7979200632T patent/DE2965681D1/en not_active Expired
- 1979-11-01 US US06/090,408 patent/US4294947A/en not_active Expired - Lifetime
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE662697A (en) * | 1965-05-20 | 1965-08-17 | ||
| DE2014172A1 (en) * | 1969-03-24 | 1970-10-29 | Phillips Petroleum Company, Bartlesville, OkIa. (V.St.A.) | Ethylene-butene copolymers with low density |
| GB1355245A (en) * | 1970-05-29 | 1974-06-05 | Mitsui Petrochemical Ind | Non-elastic ethylene copolymers and their preparation |
| DE2206429A1 (en) * | 1972-02-11 | 1973-08-30 | Huels Chemische Werke Ag | PROCESS FOR THE PRODUCTION OF LOW PRESSURE CO- AND TERPOLYMERS OF LOW DENSITY ETHYLENE |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2525612A1 (en) * | 1982-04-22 | 1983-10-28 | El Paso Polyolefins | PROCESS FOR PRODUCING LOW-DENSITY LINEAR POLYETHYLENE |
| EP0436520A1 (en) * | 1990-01-03 | 1991-07-10 | Gas Research Institute | Extended-life polyethylene gas distribution pipe |
Also Published As
| Publication number | Publication date |
|---|---|
| DE2965681D1 (en) | 1983-07-21 |
| EP0010814B1 (en) | 1983-06-15 |
| US4294947A (en) | 1981-10-13 |
| DE2847986A1 (en) | 1980-05-22 |
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